CA2196194C - Purification methods of pentafluoroethane - Google Patents
Purification methods of pentafluoroethane Download PDFInfo
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- CA2196194C CA2196194C CA002196194A CA2196194A CA2196194C CA 2196194 C CA2196194 C CA 2196194C CA 002196194 A CA002196194 A CA 002196194A CA 2196194 A CA2196194 A CA 2196194A CA 2196194 C CA2196194 C CA 2196194C
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C19/00—Acyclic saturated compounds containing halogen atoms
- C07C19/08—Acyclic saturated compounds containing halogen atoms containing fluorine
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C17/00—Preparation of halogenated hydrocarbons
- C07C17/38—Separation; Purification; Stabilisation; Use of additives
- C07C17/395—Separation; Purification; Stabilisation; Use of additives by treatment giving rise to a chemical modification of at least one compound
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J23/00—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00
- B01J23/38—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of noble metals
- B01J23/40—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of noble metals of the platinum group metals
- B01J23/44—Palladium
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C17/00—Preparation of halogenated hydrocarbons
- C07C17/23—Preparation of halogenated hydrocarbons by dehalogenation
Abstract
The purification of pentafluoroethane (HFC-125) which is composed of a process A, in which an unpurified mixture (1), containing at least chloropentafluoroethane (CFC-115) and pentafluoroethane (HFC-125) is reacted with hydrogen (4) in the presence of a catalyst in gas phase to reduce the said chloropentafluoroethane (CFC-115); and a process B, in which a reaction mixture produced by the preceding reaction is separated into a first mixture (3) composed mainly of hydrogen and a second mixture (2), composed mainly of pentafluoroethane (HFC-125). In this method, purification is performed by adding the said first mixture (3) to the said unpurified mixture (1) in a state that the hydrogen chloride is removed from the first mixture (3) in process B until the level of hydrogen chloride drops to 0.5 or less than that of CFC-115 in the unpurified mixture (1) in the molar ratio, or hydrogen chloride is removed from the said reaction mixture until, when mixed with the unpurified mixture (1), the level of hydrogen chloride drops to 0.5 or less than that of CFC-115 in the mixture in the molar ratio. Thus, CFC-115 can be exterminated (or removed) cheaply and efficiently without decreasing it's reactivity (or activity) and a high yield of HFC-125 can be obtained.
Description
Specifications Purification Methods of Pentafluoroethane Industrial fields where the invention can be utilized This invention relates to purification methods of pentafluoroethane (also referred to as HFC-125), specifically to the method of purification of HFC-125 from a mixture composed of HFC-125 which contains at least chloropentafluoroethane (also referred to as CFC-115) as a component (that is, an unpurified mixture which contains at least CFC-115 and HFC-125).
Conventional technologies HFC-125 is a chlorine-free compound and is a useful alternative to flon (chlorofluorocarbons and hydrochloro-fluorocarbons). It is used as a refrigerant, a blowing agent and a propellant.
As a method of producing the HFC-125, a method of fluorinating tetrachloroethylene is considered effective.
In this production method, however, CFC-115 is formed as a by-product. Since the boiling point of CFC-115 is -38.7 °C , and close to that of the desired product, HFC-125, -48.5 ~ , and since the relative volatility of CFC-115 to HFC-125 is near 1, it is difficult to separate them by a distillation method.
Thus, it is necessary to remove CFC-115 by another method. One of such method is to remove CFC-115 by converting it to another compound by a reduction.
Such a reduction of CFC-115 is known reaction, for example, Jap. Unexamined Pat. Publication Nos.258632/89 and 29941/92, WO 91/05752 and EP 506525 disclose methods of reducing CFC-115 by hydrogen with using mainly noble metals as catalysts. Furthermore, in WO 94/02439, a method of removing CFC-115 by converting it to HFC-125 through hydrogen reduction of HFC-125 which contains CFC-115 at temperatures between 380°~ and 500°~ in the gas phase (that is, the hydrogen reduction of CFC-115), has been disclosed.
However, in such a hydrogen reduction reaction of CFC-115, the amounts of hydrogen generally used is greater than that of CFC-115. In particular, when HFC-125 which contains CFC-115 is reduced (by the method given in WO
94/02439), the amounts of hydrogen greatly exceeds that of CFC-115. Hydrogen is very expensive, and the large amounts Z 1961. 94 of hydrogen required in the reduction process increases the cost of obtaining the desired product.
Development of the invention To resolve the above-mentioned problem, the re-use of hydrogen was considered. Extensive studies of the re-use by the inventors revealed, however, that recyclinge gas obtained after removal of HFC-125 after reduction reaction reduces reactivity considerably. This necessitates longer reaction times or higher temperatures to sustain reaction with CFC-115 until the target concentration is reached.
At the same time, if the reaction temperature is raised, the amount of multi-reduced products such as R-134a (1,1,1,2-tetrafluoroethane) or R-143a (1,1,1-trifluoroethane) increases when CFC-115 is reduced, resulting in lower yields of HFC-125; if the reaction time is made longer, both the quantity of catalyst and the volume of the reaction vessel increase, resulting in increased costs for catalysts and equipment.
Purpose of the invention The purpose of the invention is to provide a purification method for HFC-125, wherein CFC-115 can be exterminated (or removed) cheaply and efficiently without lowering the reactivity (or activity) on recycling hydrogen to produce HFC-125 in high yield, when HFC-125 containing CFC-115 is reduced with hydrogen in the gas phase.
The structure of the invention As a result of intensive studies on the recycle of gas following reduction in the above-mentioned hydrogen reduction, the inventors found that because of the presence of hydrogen chloride which is produced as a by-product during the reduction of CFC-115 in the recycle gas, it's reactivity falls sharply.
The adverse effect of hydrogen chloride was found not to be caused by an equilibrium reaction. (Therefore, even if hydrogen chloride reacts with HFC-125 under the same conditions, CFC-115 will not be produced.) Rather, it is a catalyst poison of reduction catalysts or an obstruction due to adsorption on CFC-115 reduction catalysts that decreases the activity of the catalysts. Furthermore, because higher proportions of hydrogen chloride to CFC-115 increases the adverse effect, when the concentration of CFC-115 to be reacted is low (when there is little CFC-115 in the HFC-125 to be reduced), its reactivity is markedly lower when even a small amount of hydrogen chloride is mixed.
In order to avoid such decrease in reactivity, the inventors confirmed that if the concentration of hydrogen chloride in the gas is lowered before the reacted gas is recycled, the recycle of the gas can bring about reducion of CFC-115 without lowering reactivity, then reached the invention.
That is, this invention relates to the purification method of pentafluoroethane (HFC-125) wherein, in the case of purification of the said pentafluoroethane (HFC-125) from an unpurified mixture containing at least chloro-pentafluoroethane (CFC-115) and pentafluoroethane (HFC-125), the method comprises a process A, in which the chloro-pentafluoroethane (CFC-115) is reduced by reactionwith the said unpurified mixture with hydrogen under a catalyst in the gas phase; a process B, in which thus produced reaction mixture is separated into a first mixture composed mainly of hydrogen, and a second mixture composed mainly of pentafluoroethane (HFC-125); and a process C in which hydrogen chloride is removed from the said first mixture until the quantity of hydrogen chloride becomes to be 0.5 or less than that of chloropentafluoroethane (CFC-115) in the said unpurified mixture in the molar ratio; the first mixture is then added in the said unpurified mixture, and the processes A, B and C are repeated continuously as desired.
According to this purification method, the reaction mixture can be separated into the first and second mixtures by a distillation, or a membrane separation or a pressure swing adsorption method in the process B.
Moreover, this invention also provides a purification method of pentafluoroethane (HFC-125). In the case of purification of the said pentafluoroethane (HFC-125) from an unpurified mixture containing at least chloropentafluoroethane (CFC-115) and pentafluoroethane (HFC-125), the method comprises a process I in which the said chloropentafluoroethane (CFC-115) is reduced in the said unpurified mixture with hydrogen under a catalyst in the gas phase; a process II in which, when added to the said unpurified mixture, hydrogen chloride is removed from thus produced reaction mixture until its quantity becomes 0.5 or less than that of chloropentafluoroethane (CFC-115) in the said unpurified mixture of the molar ratio; and a process III in which the reaction mixture is then separated into a first mixture composed mainly of hydrogen and a second mixture, composed mainly of pentafluoroethane (HFC-125), the first mixture then added to the said unpurified mixture, and the processes I, II, and III are repeated continuously as desired.
In this purification method, a distillation, or a membrane separation or a pressure swing adsorption method can be used to separate the reaction mixture into the first and the second mixture in the process III.
With respect to the above-mentioned purification methods based on this invention, in eitherof the method using the processes A, B and C or the method having the processes I, II and III and regarding the rate of reduction in concentration of hydrogen chloride; since the higher the concentration of hydrogen chloride, the greater the drop of the reaction rate,it was found that the concentration of hydrogen chloride should be 0.5 or less than that of CFC-115 in molarity for recycled gas, preferably be 0.1 or less in a gas mixture which is to be used in reduction reaction and contains at least CFC-115, hydrogen and HFC-125. Ideally, such mixtures should have a concentration of hydrogen chloride of 0.01 or less in the molar ratio.
That is, in the case of reacting the above-mentioned unpurified mixture under a catalyst with hydrogen in the gas phase, the molar ratio of hydrogen to chloropentafluoroethane (CFC-115) should be 5 to 200 in the above-mentioned unpurified mixture, and preferably 10 to 100; The concentration of hydrogen chloride should not be more than 0.5 that of chloropentafluoroethane (CFC-115) in the molar ratio, preferably 0.1 or less, and even more preferably 0.01 or less.
In this case, in order to reduce the concentration of hydrogen chloride (that is, to remove the hydrogen chloride substantially), this can be done by washing the mixed gas with water, or by using an alkaline solid deacidification agent.
In the purification methods based on this invention, where an unpurified mixture is to react in the gas phase with hydrogen gas, it is preferable to use a palladium and/or rhodium catalyst and to initiate the reaction of the unpurified mixture and hydrogen at temperatures between 180 ~ and 350 in the presence of a catalyst.
Below we show a flow chart describing an example of the efficient purification methods of HFC-125 based on this invention in Fig. 1, First, HFC-125 containing CFC-115 passes from (1), and hydrogen passes from (~). A reduction catalyst is filled in the reaction process(A7, Reaction temperature differs depending on the type and amount of catalyst used, the amount of CFC-115 and the amount of hydrogen, but is generally between 180 °C and 350°~ As CFC-115 is reduced in the reaction process (A), the reaction mixture that completes process (A) contains practically no CFC-115.
The reaction mixture is then sent to the HFC-125 separation process (B) and separated into a mixture (3), mainly composed of hydrogen, and a mixture (2), mainly composed of HFC-125. In this case, one method of separation can be chosen from a distillation, or a membrane separation, andapressure swing adsorption (PSA) method.
Furthermore, the mixture (3), which is mainly composed of hydrogen, is mixed with the mixture (1) which is in turn, recycled in the reduction reaction after hydrogen chloride has been removed in the hydrochloric 21 ~~619~
acid removal process (C) until concentration is 0.5 or less than that of CFC-115 in the mixture (1) in mole ratio. A removal method for hydrochloric acid (hydrogen chloride) is selected such as washing with water, or removal by the use of an alkaline solid deacidification agent.
On the other hand, the mixture (2), which is mainly composed of HFC-125, is turned into a product by rectification and other operations after the separation process (B).
The above-mentioned hydrogen chloride removal process was carried out after the separation process (B), but can also be carried out beforehand. In the latter case, process (C) can be carried out after process (A), followed by process (B). In some cases, it is possible to perform hydrogen chloride removal process after gases from (1), (3) and (4) are mixed and before the reaction process (A).
In any case, if the concentration of hydrogen chloride is reduced to 0.5 or less than that of CFC-115 in the molar ratio before the reaction process, the process will be successful.
Further, although the flow rate of each gas can incur ' various conditions, the molar raito of the hydrogen to CFC-115 before the reaction process (A) could be at least 5 to 200, preferably 10 to 100, and the molar ratio of the hydrogen chloride to CFC-115 should be 0.5 or less, preferably 0.1 or less, and ideally 0.01 or less.
With respect to the percentage of hydrogen, most is recycled in processes (A), (B) and (C). Thus, the amount of hydrogen to be newly added at (4) should correspond to the amount of CFC-115 and the amount that flows outside the process in (2), after the entire processes reach a stationary state.
Possible industrial applications This invention consists of two processes; one is that an unpurified mixture containing at least chloropentafluoroethane~(CFC-115) and pentafluoroethane (HFC-125) is made react with hydrogen in the gas phase under a catalyst to reduce the above-mentioned chloropentafluoroethane (CFC-115); and the other process is that the reaction mixture produced by the reduction is separated into a fiast mixture composed mainly of hydrogen, and a second mixture composed mainly of 2t 96194 pentafluoroethane (HFC-125). Then pentafluoroethane (HFC-125) is purified by adding the above-mentioned fist mixture to the unpurified mixture after the hydrogen chloride has been practically removed from the first mixture or from the reaction mixture. The first mixture can be added (that is, the hydrogen canbe recycled) after the hydrogen chloride, which decreasesthe reactivity of the catalyst due to a catalyst poison of the reduction catalyst or a adsorption to catalyst by CFC-115, is substantially removed. Thus, CFC-115 can be exterminated (or removed) cheaply and efficiently without decreasing it's reactivity (or activity), and high yields of HFC-125 can be obtained.
Brief explanation of figure Fig. 1 is a flow chart which illustrates an example of the purification methods of HFC-125 based on this invention.
Explanation of symbols (1) HFC-125 containing CFC-115 (2) A mixture composed mainly of HFC-125 (3) A mixture composed mainly of hydrogen (4) Hydrogen (A) Reduction of CFC-115 (B) Separation of HFC-125 (C) Removal of hydrochloric acid (hydrogen chloride) Examples This invention will be explained in detail in the following examples, making~comparisons to other methods, but the applications of the method are not limitted to such examples.
Comparative example 1 A stainless steel reaction tube 15 mm in inside diameter was filled with 10 g of a rhodium catalyst, carried on active carbon by 3 wt.~. Hydrogen, CFC-115 and HFC-125 were passed through the tube at a rate of 45 cc/min., 1.9 cc/min. and 56.1 cc/min. respectively to be reacted at a reaction temperature of 250°C
Analysis of the product at the outlet of the reaction tube by gas chromatograph did not detect CFC-115. The reaction mixture was then passed through a membrane to separate the HFC-125.
ZI ~bj 9~
After the HFC-125 was separated, the remaining gas contained hydrogen, hydrogen chloride and HFC-125 at a mole ratio of 90:3.8:6.2.
50 cc/min. of this mixture was added to 1.9 cc/min.
CFC-115 and 50 cc/min. HFC-125 and again passed through the stainless steel reaction tube 15 mm in inside diameter which was filled with 10 g of a rhodium catalyst carried on active carbon by 3wt.~. The mixture was made to react at 250 .
The concentration of CFC-115 at the inlet of the reaction tube was CFC-115/(CFC-115 + HFC-125)=3.2~, while the CFC-115 concentration at the outlet of the reaction tube was CFC-115/(CFC-115 + HFC-125)=0.3~.
Example l A stainless steel reaction tube 15 mm in inside diameter was filled with 10 g of a rhodium catalyst carried on active carbon by 3 wt.~. Hydrogen, CFC-115 and HFC-125 were passed at a rateof 45 cc/min., 1.9 cc/min.
and 56.1 cc/min. respectively to be reacted at a reaction temperature of 250°C .
Analysis of the product at the outlet of the reaction 2l 9b~ ~4 tube by a gas chromatograph revealed no CFC-115. The mixture was washed with water to remove the hydrogen chloride and dried. The concentration of hydrogen chloride was 0.1% of the HFC-125 in mole ratio.
The mixture was then passed through a membrane to separate the HFC-125 and hydrogen. The mixture which was separated by the membrane device was composed mainly of hydrogen, and also contained hydrogen chloride and HFC-125 at a mole ratio of 93.6:0.1:6.3.
50 cc/min. of this mixture was added to 1.9 cc/min.
CFC-115 and 50 cc/min. HFC-125 and passed through the above-mentioned stainless steel reaction tube 15 mm in inside diameter which was filled with 10 g of a rhodium catalyst carried on active carbon by 3 wt.~. The mixture was made to react at 250°C .
At the inlet of the reaction tube, CFC-115/(CFC-115 +
HFC-125) was 3.4yb, while at the outlet of the reaction tube, CFC-115 was not detected.
Examples 2 and 3, comparative examples 2 to 5 Reactions were carried out similarly, except that the ratio of CFC-115 to hydrogen chloride in the mixture used in the reaction and the type of catalyst were changed as indicated in examples 2 and 3 in Table-1 based on example 1, and as indicated in comparative examples 2 to 5 in Table-1 based on comparative example 1. The percentages of CFC-115/(CFC-115 + HFC-125) after reduction are shown in the following Table-1.
+
., ..
c~ o ~r 0 0 .-i o o ri +; \ n td .-~ c~ C~ ~-, c~ cn ...
.-~r o~ oo h- o~ oo h-F3 ,~~"~
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A
a ~ N c0 N 00 ~
..
.., -a 5 O v-i Gfl O ri tD
.C
~
,~ ~ a N
~ ~ i 'N ~
' ~''~
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, a~
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'~ ~ ~4 t~ ~ a~
,~
a s ..~
, ~.
m oa oo ~i a> ., R Q
'~ ~ ~ ~ i ~ ~
, A A
_ __ N ~ ~ C~J -~ --r ~ Y ~
N C~ ~ t!7 \
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. .~ ~ ~ .
i ., ., +
. .
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.
~1 X6194 Results show that the reduction of CFC-115 depends greatly on the concentration of hydrochloric acid (hydrogen chloride), and that CFC-115 can be completely removed if the reaction is performed after hydrochloric acid is substantially removed using this invention. On the other hand, the reduction of CFC-115 is inhibited as shown in the comparative examples when the reaction is carried out without removal of hydrochloric acid.
Example 4 A stainless steel reaction tube 15 mm in inside diameter was filled with 10 g of a rhodium catalyst carried on active carbon by 3 wt.%. Hydrogen, CFC-115 and HFC-125 were passed through at a rate of 45 cc/min., 1.9 cc/min. and 56.1 cc/min. respectively to be reacted at a reaction temperature of 250 °C .
Analysis of the reaction product at the outlet of the reaction tube by gas chromatograph did not detect CFC-115.
The mixture was then passed through a membrane to separate the HFC-125.
After the HFC-125 was separated, the remaining mixture was washed with water and dried. The resulting gas 21 ~~i 94 contained hydrogen, hydrogen chloride and HFC-125 at a mole ratio of 93.6:0.01:6.4.
50 cc/min. of the mixture was added to 1.9 cc/min. of CFC-115 and 50 cc/min. of HFC-125 and again passed through the stainless steel reaction tube, 15 mm in inside diameter with 10 g of rhodium catalyst carried on active carbon by 3 wt.%. The mixture was made to react at 250°C .
The percentage of CFC-.115 at the inlet of the reaction tube was CFC-115/(CFC-115 + HFC-125)=3.4 % and CFC-115 was not detected at the outlet of the reaction tube.
Reference example 1 A stainless steel reaction tube 15 mm in inside diameter was filled with 10 g rhodium catalyst carried on active carbon by 3 wt.~. Hydrogen chloride and HFC-125 were passed through the tube at a rate of 10 cc/min. and 100 cc/min. respectively to be reacted at a reaction temperature of 250 ~ .
Analysis of the product at the outlet of the reaction tube by a gas chromatograph revealed no CFC-115. The HFC-125 and HC1 did not react.
Conventional technologies HFC-125 is a chlorine-free compound and is a useful alternative to flon (chlorofluorocarbons and hydrochloro-fluorocarbons). It is used as a refrigerant, a blowing agent and a propellant.
As a method of producing the HFC-125, a method of fluorinating tetrachloroethylene is considered effective.
In this production method, however, CFC-115 is formed as a by-product. Since the boiling point of CFC-115 is -38.7 °C , and close to that of the desired product, HFC-125, -48.5 ~ , and since the relative volatility of CFC-115 to HFC-125 is near 1, it is difficult to separate them by a distillation method.
Thus, it is necessary to remove CFC-115 by another method. One of such method is to remove CFC-115 by converting it to another compound by a reduction.
Such a reduction of CFC-115 is known reaction, for example, Jap. Unexamined Pat. Publication Nos.258632/89 and 29941/92, WO 91/05752 and EP 506525 disclose methods of reducing CFC-115 by hydrogen with using mainly noble metals as catalysts. Furthermore, in WO 94/02439, a method of removing CFC-115 by converting it to HFC-125 through hydrogen reduction of HFC-125 which contains CFC-115 at temperatures between 380°~ and 500°~ in the gas phase (that is, the hydrogen reduction of CFC-115), has been disclosed.
However, in such a hydrogen reduction reaction of CFC-115, the amounts of hydrogen generally used is greater than that of CFC-115. In particular, when HFC-125 which contains CFC-115 is reduced (by the method given in WO
94/02439), the amounts of hydrogen greatly exceeds that of CFC-115. Hydrogen is very expensive, and the large amounts Z 1961. 94 of hydrogen required in the reduction process increases the cost of obtaining the desired product.
Development of the invention To resolve the above-mentioned problem, the re-use of hydrogen was considered. Extensive studies of the re-use by the inventors revealed, however, that recyclinge gas obtained after removal of HFC-125 after reduction reaction reduces reactivity considerably. This necessitates longer reaction times or higher temperatures to sustain reaction with CFC-115 until the target concentration is reached.
At the same time, if the reaction temperature is raised, the amount of multi-reduced products such as R-134a (1,1,1,2-tetrafluoroethane) or R-143a (1,1,1-trifluoroethane) increases when CFC-115 is reduced, resulting in lower yields of HFC-125; if the reaction time is made longer, both the quantity of catalyst and the volume of the reaction vessel increase, resulting in increased costs for catalysts and equipment.
Purpose of the invention The purpose of the invention is to provide a purification method for HFC-125, wherein CFC-115 can be exterminated (or removed) cheaply and efficiently without lowering the reactivity (or activity) on recycling hydrogen to produce HFC-125 in high yield, when HFC-125 containing CFC-115 is reduced with hydrogen in the gas phase.
The structure of the invention As a result of intensive studies on the recycle of gas following reduction in the above-mentioned hydrogen reduction, the inventors found that because of the presence of hydrogen chloride which is produced as a by-product during the reduction of CFC-115 in the recycle gas, it's reactivity falls sharply.
The adverse effect of hydrogen chloride was found not to be caused by an equilibrium reaction. (Therefore, even if hydrogen chloride reacts with HFC-125 under the same conditions, CFC-115 will not be produced.) Rather, it is a catalyst poison of reduction catalysts or an obstruction due to adsorption on CFC-115 reduction catalysts that decreases the activity of the catalysts. Furthermore, because higher proportions of hydrogen chloride to CFC-115 increases the adverse effect, when the concentration of CFC-115 to be reacted is low (when there is little CFC-115 in the HFC-125 to be reduced), its reactivity is markedly lower when even a small amount of hydrogen chloride is mixed.
In order to avoid such decrease in reactivity, the inventors confirmed that if the concentration of hydrogen chloride in the gas is lowered before the reacted gas is recycled, the recycle of the gas can bring about reducion of CFC-115 without lowering reactivity, then reached the invention.
That is, this invention relates to the purification method of pentafluoroethane (HFC-125) wherein, in the case of purification of the said pentafluoroethane (HFC-125) from an unpurified mixture containing at least chloro-pentafluoroethane (CFC-115) and pentafluoroethane (HFC-125), the method comprises a process A, in which the chloro-pentafluoroethane (CFC-115) is reduced by reactionwith the said unpurified mixture with hydrogen under a catalyst in the gas phase; a process B, in which thus produced reaction mixture is separated into a first mixture composed mainly of hydrogen, and a second mixture composed mainly of pentafluoroethane (HFC-125); and a process C in which hydrogen chloride is removed from the said first mixture until the quantity of hydrogen chloride becomes to be 0.5 or less than that of chloropentafluoroethane (CFC-115) in the said unpurified mixture in the molar ratio; the first mixture is then added in the said unpurified mixture, and the processes A, B and C are repeated continuously as desired.
According to this purification method, the reaction mixture can be separated into the first and second mixtures by a distillation, or a membrane separation or a pressure swing adsorption method in the process B.
Moreover, this invention also provides a purification method of pentafluoroethane (HFC-125). In the case of purification of the said pentafluoroethane (HFC-125) from an unpurified mixture containing at least chloropentafluoroethane (CFC-115) and pentafluoroethane (HFC-125), the method comprises a process I in which the said chloropentafluoroethane (CFC-115) is reduced in the said unpurified mixture with hydrogen under a catalyst in the gas phase; a process II in which, when added to the said unpurified mixture, hydrogen chloride is removed from thus produced reaction mixture until its quantity becomes 0.5 or less than that of chloropentafluoroethane (CFC-115) in the said unpurified mixture of the molar ratio; and a process III in which the reaction mixture is then separated into a first mixture composed mainly of hydrogen and a second mixture, composed mainly of pentafluoroethane (HFC-125), the first mixture then added to the said unpurified mixture, and the processes I, II, and III are repeated continuously as desired.
In this purification method, a distillation, or a membrane separation or a pressure swing adsorption method can be used to separate the reaction mixture into the first and the second mixture in the process III.
With respect to the above-mentioned purification methods based on this invention, in eitherof the method using the processes A, B and C or the method having the processes I, II and III and regarding the rate of reduction in concentration of hydrogen chloride; since the higher the concentration of hydrogen chloride, the greater the drop of the reaction rate,it was found that the concentration of hydrogen chloride should be 0.5 or less than that of CFC-115 in molarity for recycled gas, preferably be 0.1 or less in a gas mixture which is to be used in reduction reaction and contains at least CFC-115, hydrogen and HFC-125. Ideally, such mixtures should have a concentration of hydrogen chloride of 0.01 or less in the molar ratio.
That is, in the case of reacting the above-mentioned unpurified mixture under a catalyst with hydrogen in the gas phase, the molar ratio of hydrogen to chloropentafluoroethane (CFC-115) should be 5 to 200 in the above-mentioned unpurified mixture, and preferably 10 to 100; The concentration of hydrogen chloride should not be more than 0.5 that of chloropentafluoroethane (CFC-115) in the molar ratio, preferably 0.1 or less, and even more preferably 0.01 or less.
In this case, in order to reduce the concentration of hydrogen chloride (that is, to remove the hydrogen chloride substantially), this can be done by washing the mixed gas with water, or by using an alkaline solid deacidification agent.
In the purification methods based on this invention, where an unpurified mixture is to react in the gas phase with hydrogen gas, it is preferable to use a palladium and/or rhodium catalyst and to initiate the reaction of the unpurified mixture and hydrogen at temperatures between 180 ~ and 350 in the presence of a catalyst.
Below we show a flow chart describing an example of the efficient purification methods of HFC-125 based on this invention in Fig. 1, First, HFC-125 containing CFC-115 passes from (1), and hydrogen passes from (~). A reduction catalyst is filled in the reaction process(A7, Reaction temperature differs depending on the type and amount of catalyst used, the amount of CFC-115 and the amount of hydrogen, but is generally between 180 °C and 350°~ As CFC-115 is reduced in the reaction process (A), the reaction mixture that completes process (A) contains practically no CFC-115.
The reaction mixture is then sent to the HFC-125 separation process (B) and separated into a mixture (3), mainly composed of hydrogen, and a mixture (2), mainly composed of HFC-125. In this case, one method of separation can be chosen from a distillation, or a membrane separation, andapressure swing adsorption (PSA) method.
Furthermore, the mixture (3), which is mainly composed of hydrogen, is mixed with the mixture (1) which is in turn, recycled in the reduction reaction after hydrogen chloride has been removed in the hydrochloric 21 ~~619~
acid removal process (C) until concentration is 0.5 or less than that of CFC-115 in the mixture (1) in mole ratio. A removal method for hydrochloric acid (hydrogen chloride) is selected such as washing with water, or removal by the use of an alkaline solid deacidification agent.
On the other hand, the mixture (2), which is mainly composed of HFC-125, is turned into a product by rectification and other operations after the separation process (B).
The above-mentioned hydrogen chloride removal process was carried out after the separation process (B), but can also be carried out beforehand. In the latter case, process (C) can be carried out after process (A), followed by process (B). In some cases, it is possible to perform hydrogen chloride removal process after gases from (1), (3) and (4) are mixed and before the reaction process (A).
In any case, if the concentration of hydrogen chloride is reduced to 0.5 or less than that of CFC-115 in the molar ratio before the reaction process, the process will be successful.
Further, although the flow rate of each gas can incur ' various conditions, the molar raito of the hydrogen to CFC-115 before the reaction process (A) could be at least 5 to 200, preferably 10 to 100, and the molar ratio of the hydrogen chloride to CFC-115 should be 0.5 or less, preferably 0.1 or less, and ideally 0.01 or less.
With respect to the percentage of hydrogen, most is recycled in processes (A), (B) and (C). Thus, the amount of hydrogen to be newly added at (4) should correspond to the amount of CFC-115 and the amount that flows outside the process in (2), after the entire processes reach a stationary state.
Possible industrial applications This invention consists of two processes; one is that an unpurified mixture containing at least chloropentafluoroethane~(CFC-115) and pentafluoroethane (HFC-125) is made react with hydrogen in the gas phase under a catalyst to reduce the above-mentioned chloropentafluoroethane (CFC-115); and the other process is that the reaction mixture produced by the reduction is separated into a fiast mixture composed mainly of hydrogen, and a second mixture composed mainly of 2t 96194 pentafluoroethane (HFC-125). Then pentafluoroethane (HFC-125) is purified by adding the above-mentioned fist mixture to the unpurified mixture after the hydrogen chloride has been practically removed from the first mixture or from the reaction mixture. The first mixture can be added (that is, the hydrogen canbe recycled) after the hydrogen chloride, which decreasesthe reactivity of the catalyst due to a catalyst poison of the reduction catalyst or a adsorption to catalyst by CFC-115, is substantially removed. Thus, CFC-115 can be exterminated (or removed) cheaply and efficiently without decreasing it's reactivity (or activity), and high yields of HFC-125 can be obtained.
Brief explanation of figure Fig. 1 is a flow chart which illustrates an example of the purification methods of HFC-125 based on this invention.
Explanation of symbols (1) HFC-125 containing CFC-115 (2) A mixture composed mainly of HFC-125 (3) A mixture composed mainly of hydrogen (4) Hydrogen (A) Reduction of CFC-115 (B) Separation of HFC-125 (C) Removal of hydrochloric acid (hydrogen chloride) Examples This invention will be explained in detail in the following examples, making~comparisons to other methods, but the applications of the method are not limitted to such examples.
Comparative example 1 A stainless steel reaction tube 15 mm in inside diameter was filled with 10 g of a rhodium catalyst, carried on active carbon by 3 wt.~. Hydrogen, CFC-115 and HFC-125 were passed through the tube at a rate of 45 cc/min., 1.9 cc/min. and 56.1 cc/min. respectively to be reacted at a reaction temperature of 250°C
Analysis of the product at the outlet of the reaction tube by gas chromatograph did not detect CFC-115. The reaction mixture was then passed through a membrane to separate the HFC-125.
ZI ~bj 9~
After the HFC-125 was separated, the remaining gas contained hydrogen, hydrogen chloride and HFC-125 at a mole ratio of 90:3.8:6.2.
50 cc/min. of this mixture was added to 1.9 cc/min.
CFC-115 and 50 cc/min. HFC-125 and again passed through the stainless steel reaction tube 15 mm in inside diameter which was filled with 10 g of a rhodium catalyst carried on active carbon by 3wt.~. The mixture was made to react at 250 .
The concentration of CFC-115 at the inlet of the reaction tube was CFC-115/(CFC-115 + HFC-125)=3.2~, while the CFC-115 concentration at the outlet of the reaction tube was CFC-115/(CFC-115 + HFC-125)=0.3~.
Example l A stainless steel reaction tube 15 mm in inside diameter was filled with 10 g of a rhodium catalyst carried on active carbon by 3 wt.~. Hydrogen, CFC-115 and HFC-125 were passed at a rateof 45 cc/min., 1.9 cc/min.
and 56.1 cc/min. respectively to be reacted at a reaction temperature of 250°C .
Analysis of the product at the outlet of the reaction 2l 9b~ ~4 tube by a gas chromatograph revealed no CFC-115. The mixture was washed with water to remove the hydrogen chloride and dried. The concentration of hydrogen chloride was 0.1% of the HFC-125 in mole ratio.
The mixture was then passed through a membrane to separate the HFC-125 and hydrogen. The mixture which was separated by the membrane device was composed mainly of hydrogen, and also contained hydrogen chloride and HFC-125 at a mole ratio of 93.6:0.1:6.3.
50 cc/min. of this mixture was added to 1.9 cc/min.
CFC-115 and 50 cc/min. HFC-125 and passed through the above-mentioned stainless steel reaction tube 15 mm in inside diameter which was filled with 10 g of a rhodium catalyst carried on active carbon by 3 wt.~. The mixture was made to react at 250°C .
At the inlet of the reaction tube, CFC-115/(CFC-115 +
HFC-125) was 3.4yb, while at the outlet of the reaction tube, CFC-115 was not detected.
Examples 2 and 3, comparative examples 2 to 5 Reactions were carried out similarly, except that the ratio of CFC-115 to hydrogen chloride in the mixture used in the reaction and the type of catalyst were changed as indicated in examples 2 and 3 in Table-1 based on example 1, and as indicated in comparative examples 2 to 5 in Table-1 based on comparative example 1. The percentages of CFC-115/(CFC-115 + HFC-125) after reduction are shown in the following Table-1.
+
., ..
c~ o ~r 0 0 .-i o o ri +; \ n td .-~ c~ C~ ~-, c~ cn ...
.-~r o~ oo h- o~ oo h-F3 ,~~"~
r1 r-1 r1 rl ri rl V K
A
a ~ N c0 N 00 ~
..
.., -a 5 O v-i Gfl O ri tD
.C
~
,~ ~ a N
~ ~ i 'N ~
' ~''~
V c a~
, a~
co b --~
'~ ~ ~4 t~ ~ a~
,~
a s ..~
, ~.
m oa oo ~i a> ., R Q
'~ ~ ~ ~ i ~ ~
, A A
_ __ N ~ ~ C~J -~ --r ~ Y ~
N C~ ~ t!7 \
d ~ ~ 4 4 4 ~
. .~ ~ ~ .
i ., ., +
. .
i a V
F' ~ ~ ~ a~ ~ caa H .~ pa ~ t~
.
~1 X6194 Results show that the reduction of CFC-115 depends greatly on the concentration of hydrochloric acid (hydrogen chloride), and that CFC-115 can be completely removed if the reaction is performed after hydrochloric acid is substantially removed using this invention. On the other hand, the reduction of CFC-115 is inhibited as shown in the comparative examples when the reaction is carried out without removal of hydrochloric acid.
Example 4 A stainless steel reaction tube 15 mm in inside diameter was filled with 10 g of a rhodium catalyst carried on active carbon by 3 wt.%. Hydrogen, CFC-115 and HFC-125 were passed through at a rate of 45 cc/min., 1.9 cc/min. and 56.1 cc/min. respectively to be reacted at a reaction temperature of 250 °C .
Analysis of the reaction product at the outlet of the reaction tube by gas chromatograph did not detect CFC-115.
The mixture was then passed through a membrane to separate the HFC-125.
After the HFC-125 was separated, the remaining mixture was washed with water and dried. The resulting gas 21 ~~i 94 contained hydrogen, hydrogen chloride and HFC-125 at a mole ratio of 93.6:0.01:6.4.
50 cc/min. of the mixture was added to 1.9 cc/min. of CFC-115 and 50 cc/min. of HFC-125 and again passed through the stainless steel reaction tube, 15 mm in inside diameter with 10 g of rhodium catalyst carried on active carbon by 3 wt.%. The mixture was made to react at 250°C .
The percentage of CFC-.115 at the inlet of the reaction tube was CFC-115/(CFC-115 + HFC-125)=3.4 % and CFC-115 was not detected at the outlet of the reaction tube.
Reference example 1 A stainless steel reaction tube 15 mm in inside diameter was filled with 10 g rhodium catalyst carried on active carbon by 3 wt.~. Hydrogen chloride and HFC-125 were passed through the tube at a rate of 10 cc/min. and 100 cc/min. respectively to be reacted at a reaction temperature of 250 ~ .
Analysis of the product at the outlet of the reaction tube by a gas chromatograph revealed no CFC-115. The HFC-125 and HC1 did not react.
Claims (14)
1. A method for the purification of pentafluoroethane from an unpurified mixture containing at least chloropentafluoroethane as an impurity, the method comprising:
(a) reacting the chloropentafluoroethane with hydrogen in the presence of a catalyst in gas phase so as to obtain a reaction mixture consisting of a non-organic mixture and a product, the non-organic mixture consisting essentially of hydrogen and hydrogen chloride, and the product consisting essentially of pentatluoroethane;
(b) separating the product from the non-organic mixture; and (c) removing the hydrogen chloride from the non-organic mixture and recycling the non-organic mixture to the unpurified mixture until concentration of hydrogen chloride is 0.5 or less than that of chloropentafluoroethane in the molar ratio in the unpurified mixture.
(a) reacting the chloropentafluoroethane with hydrogen in the presence of a catalyst in gas phase so as to obtain a reaction mixture consisting of a non-organic mixture and a product, the non-organic mixture consisting essentially of hydrogen and hydrogen chloride, and the product consisting essentially of pentatluoroethane;
(b) separating the product from the non-organic mixture; and (c) removing the hydrogen chloride from the non-organic mixture and recycling the non-organic mixture to the unpurified mixture until concentration of hydrogen chloride is 0.5 or less than that of chloropentafluoroethane in the molar ratio in the unpurified mixture.
2. The purification method as defined in claim 1, in which the process steps (a), (b) and (c) are continuously repeated.
3. The purification method as defined in claim 1 or 2, in which the reaction mixture is separated in process step (b) by distillation.
4. The purification method as defined in claim 1 or 2, in which the reaction mixture is separated in process step (b) by a membrane separation method.
5. The purification method as defined in claim 1 or 2, in which the reaction mixture is separated in process step (b) by a pressure swing adsorption method.
6. A method for the purification of pentafluoroethane from an unpurified mixture containing at least chloropentafluoroethane as an impurity, the method comprising:
I. reacting the chloropentafluoroethane with hydrogen in the presence of a catalyst in gas phase so as to obtain a reaction mixture consisting of a non-organic mixture and a product, the non-organic mixture consisting essentially of hydrogen and hydrogen chloride, and the product consisting essentially of pentafluoroethane;
II. removing the hydrogen chloride from the reaction mixture and recycling the reaction mixture to the unpurified mixture until concentration of hydrogen chloride is 0.5 or less than that of chloropentafluoroethane in the molar ratio in the unpurified mixture; and III. separating the product from the non-organic mixture.
I. reacting the chloropentafluoroethane with hydrogen in the presence of a catalyst in gas phase so as to obtain a reaction mixture consisting of a non-organic mixture and a product, the non-organic mixture consisting essentially of hydrogen and hydrogen chloride, and the product consisting essentially of pentafluoroethane;
II. removing the hydrogen chloride from the reaction mixture and recycling the reaction mixture to the unpurified mixture until concentration of hydrogen chloride is 0.5 or less than that of chloropentafluoroethane in the molar ratio in the unpurified mixture; and III. separating the product from the non-organic mixture.
7. The purification method as defined in claim 6, in which the process steps I, II and III are continuously repeated.
8. The purification method as defined in claim 6 or 7, in which the reaction mixture is separated in process step III by distillation.
9. The purification method as defined in claim 6 or 7, in which the reaction mixture is separated in process step III by a membrane separation method.
10. The purification method as defined in claim 6 or 7, in which the reaction mixture is separated in process step III by a pressure swing adsorption method.
11. The purification method as defined in one of claims 1 to 10, in which when the unpurified mixture is made to react with hydrogen in the presence of a catalyst in gas phase, the molar ratio of hydrogen to chloropentafluoroethane is between 5 and 200.
12. The purification method as defined in one of claims 1 to 10, in which when the unpurified mixture is made to react with hydrogen in the presence of a catalyst in gas phase, the concentration of hydrogen chloride is 0.5 or less than that of chloropentafluoroethane in the molar ratio in the said unpurified mixture.
13. The purification method as defined in one of claims 1 to 10, in which in the case of the reaction between the unpurified mixture and hydrogen in gas phase, a catalyst carrying palladium and/or rhodium is used.
14. The purification method as defined in one of claims 1 to 10, in which the unpurified mixture is made to react with hydrogen in the presence of a catalyst at temperature between 180°C and 350°C.
Applications Claiming Priority (3)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP198019/1994 | 1994-07-29 | ||
| JP19801994A JP3491702B2 (en) | 1994-07-29 | 1994-07-29 | Method for purifying pentafluoroethane |
| PCT/JP1995/001488 WO1996004226A1 (en) | 1994-07-29 | 1995-07-25 | Method of purifying pentafluoroethane |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CA2196194A1 CA2196194A1 (en) | 1996-02-15 |
| CA2196194C true CA2196194C (en) | 2000-04-04 |
Family
ID=16384173
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CA002196194A Expired - Fee Related CA2196194C (en) | 1994-07-29 | 1995-07-25 | Purification methods of pentafluoroethane |
Country Status (12)
| Country | Link |
|---|---|
| US (1) | US5852223A (en) |
| EP (1) | EP0773207B1 (en) |
| JP (1) | JP3491702B2 (en) |
| KR (1) | KR100232038B1 (en) |
| CN (1) | CN1059660C (en) |
| AT (1) | ATE193279T1 (en) |
| AU (1) | AU679388B2 (en) |
| BR (1) | BR9508448B1 (en) |
| CA (1) | CA2196194C (en) |
| DE (1) | DE69517182T2 (en) |
| RU (1) | RU2131407C1 (en) |
| WO (1) | WO1996004226A1 (en) |
Families Citing this family (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| FR2752836B1 (en) * | 1996-08-30 | 1998-10-30 | Atochem Elf Sa | PURIFICATION OF PENTAFLUOROETHANE |
| US11274069B2 (en) | 2020-08-13 | 2022-03-15 | L'Air Liquide, Société Anonyme pour l'Etude et l'Exploitation des Procédés Georges Claude | Mono-substituted cyclopentadienes and metal cyclopentadienyl complexes and synthesis methods thereof |
| FR3131305A1 (en) * | 2021-12-23 | 2023-06-30 | Arkema France | Process for the production and purification of trifluoroethylene |
Family Cites Families (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| GB1578933A (en) * | 1977-05-24 | 1980-11-12 | Ici Ltd | Manufacture of halogenated hydrocarbons |
| JP2814606B2 (en) * | 1989-09-12 | 1998-10-27 | 旭硝子株式会社 | Method for producing pentafluoroethane |
| JPH0426636A (en) * | 1990-05-22 | 1992-01-29 | Asahi Glass Co Ltd | Reduction of halogenated carbon |
| EP0651733A1 (en) * | 1992-07-22 | 1995-05-10 | Imperial Chemical Industries Plc | Purification of pentafluoroethane |
-
1994
- 1994-07-29 JP JP19801994A patent/JP3491702B2/en not_active Expired - Fee Related
-
1995
- 1995-07-25 US US08/776,194 patent/US5852223A/en not_active Expired - Fee Related
- 1995-07-25 AU AU30863/95A patent/AU679388B2/en not_active Ceased
- 1995-07-25 DE DE69517182T patent/DE69517182T2/en not_active Expired - Fee Related
- 1995-07-25 AT AT95926503T patent/ATE193279T1/en active
- 1995-07-25 EP EP95926503A patent/EP0773207B1/en not_active Expired - Lifetime
- 1995-07-25 CA CA002196194A patent/CA2196194C/en not_active Expired - Fee Related
- 1995-07-25 WO PCT/JP1995/001488 patent/WO1996004226A1/en active IP Right Grant
- 1995-07-25 CN CN95194357A patent/CN1059660C/en not_active Expired - Fee Related
- 1995-07-25 BR BRPI9508448-7A patent/BR9508448B1/en not_active IP Right Cessation
- 1995-07-25 RU RU97103332A patent/RU2131407C1/en not_active IP Right Cessation
- 1995-07-25 KR KR1019970700604A patent/KR100232038B1/en not_active IP Right Cessation
Also Published As
| Publication number | Publication date |
|---|---|
| EP0773207B1 (en) | 2000-05-24 |
| CN1154099A (en) | 1997-07-09 |
| US5852223A (en) | 1998-12-22 |
| JP3491702B2 (en) | 2004-01-26 |
| JPH0840949A (en) | 1996-02-13 |
| KR970704652A (en) | 1997-09-06 |
| DE69517182D1 (en) | 2000-06-29 |
| EP0773207A4 (en) | 1997-06-18 |
| AU679388B2 (en) | 1997-06-26 |
| ATE193279T1 (en) | 2000-06-15 |
| CA2196194A1 (en) | 1996-02-15 |
| BR9508448B1 (en) | 2011-02-22 |
| BR9508448A (en) | 1997-10-28 |
| AU3086395A (en) | 1996-03-04 |
| EP0773207A1 (en) | 1997-05-14 |
| RU2131407C1 (en) | 1999-06-10 |
| CN1059660C (en) | 2000-12-20 |
| DE69517182T2 (en) | 2001-01-25 |
| WO1996004226A1 (en) | 1996-02-15 |
| KR100232038B1 (en) | 1999-12-01 |
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